CN2815487Y - Internal back streaming tower fluidized_bed reactor with habyrinth helical fin diversion baffle - Google Patents
Internal back streaming tower fluidized_bed reactor with habyrinth helical fin diversion baffle Download PDFInfo
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- CN2815487Y CN2815487Y CN 200520035081 CN200520035081U CN2815487Y CN 2815487 Y CN2815487 Y CN 2815487Y CN 200520035081 CN200520035081 CN 200520035081 CN 200520035081 U CN200520035081 U CN 200520035081U CN 2815487 Y CN2815487 Y CN 2815487Y
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- bed reactor
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Abstract
The utility model provides an internal back-streaming tower type fluidized-bed reactor with a labyrinth helical fin diversion baffle, which comprises a tower body (1) with a reaction bed distribution plate (4), a material inlet (2) positioned on the tower body, a discharge hole (5), an air current inlet (6), an air current outlet (13) and a material revert opening (8). The utility model is characterized in that a labyrinth helical fin diversion baffle (3) which is composed of a plurality of helical fins (17) is distributed on an inner wall of the tower body. Under the action of the labyrinth helical fin diversion baffle, spiral air current formed carries out centrifugal separation on suspended solid material above a reaction bed, downward internal return flow is formed along the labyrinth helical fin diversion baffle, the flow speed of the air current is increased, the internal return flow of the solid material is increased, the reaction efficiency of fluidization is also increased and granules which are output out of the tower in the form of dilute phase are reduced. The utility model can effectively control the dense phase height of material in fluidized state and the distribution proportion of material phase at each level, can improve the mixing effect of gas-solid phase, and has the advantages of simple structure, low fabrication cost, small material return quantity of outer circulation and small power loss of the air current.
Description
Technical field:
The utility model is relevant with fluidized-bed reactor, special be with labyrinth helical fin flow apron in the tower fluidized-bed reactor that backflows relevant.
Background technology:
Fluidized-bed reactor is the exemplary apparatus of gas one solid phase (powder) reaction, its reaction principle is that powder material is back to back in tower reactor, under the air-flow that contains gas phase media promotes, make solid phase particles break through the sedimentation critical point, be higher than its free-falling velocity low suspension, under the condition of the confined space, make that the microcosmic surface of particle is maximized to contact and finish reaction with gas phase media.The reaction efficiency of fluidized-bed reactor depends on following condition:
1, finishes controllable fluidisation attitude, adjust gas speed, make the thing of conversion zone be in even and stable suspended state mutually, the subparticle content of transportation section is minimized, reach the purpose that dilute phase is carried.
2, finish controllable solid-phase material turnover balance, the adjustment solid phase is got material level and is put and pass in and out flow, makes the material level of conversion zone be in stable state.
3, finish controllable hot merit balance, adjust the heat supply or adjust available heat of gasification, or heat exchange component in the tower is set, finish the required optimal temperature conditions of reaction.
4, finish controllable environment discharge capacity, exteenal reflux makes gas one solid phase reaction maximizing efficiency in utilizing, and discharge of poisonous waste is minimized.
In the present tower stream of fine particles fluidized bed reactor tower heat exchange internals often are set, tower disposes multi-cyclone outward and finishes the outer circulation returning charge, and its shortcoming is a complex structure, and the shop helps equipment many, and outer circulation returning charge amount is big, and easily stifled, the air-flow kinetic equation loss is big.
The utility model content:
The purpose of this utility model is in order to overcome above deficiency, provide a kind of simple in structure, cost is low, can effectively control the concentrated phase height and each aspect thing distribution proportion mutually of fluidisation attitude material, improve gas---the mixed effect of solid phase, outer circulation returning charge amount is little, and tower fluidized-bed reactor backflows in the band labyrinth helical fin flow apron that the air-flow kinetic equation loss is little.
The purpose of this utility model is achieved like this:
Tower fluidized-bed reactor backflows in the helical fin flow apron of the utility model band labyrinth, the tower body that comprises band reaction bed distribution grid, be positioned at material inlet, discharging opening, airflow inlet, air stream outlet and material returning charge mouth on the tower body, it is characterized in that being distributed with on the tower body inwall labyrinth helical fin flow apron that forms by some helical fins.
Above-mentioned some helical fin water conservancy diversion are broken into the labyrinth and distribute.
Above-mentioned helical fin is the hollow-core construction of bringing into, exporting, and connects with the tower body inwall, advances to feed refrigerant in cavity, can adjust the tower interior reaction temperature effectively.
Above-mentioned helical fin is a solid construction.
Above-mentioned labyrinth helical fin flow apron is positioned on the tower body material returning charge mouth.
Above-mentioned material returning charge mouth is arranged on the conversion zone of tower body hypomere.
Above-mentioned air stream outlet is located at the tower body top center, and air flow outlet has the cyclone separator that is communicated with it.
The tower fluidized-bed reactor that backflows in the helical fin flow apron of the utility model band labyrinth is provided with the labyrinth helical fin flow apron of being made up of some helical fins on the tower body inwall, make the parallel airflow field in the tower body become the spiral air flow field, solid matter (powder) when making reaction forms cyclonic separation in tower body, finish the returning charge amount more than 90%.Only a cyclone separator need be set outside tower body separates subparticle.The distributions of the helical angle of labyrinth helical fin flow apron, spiral plate width, spiral plate etc. can be provided with according to the physical characteristic (as granularity, proportion, apparent specific gravity (gd), particle shape etc.) of different material, the factors such as requirement, tower body diameter and length of reactiveness.
Compare with existing tower stream of fine particles fluidized bed reactor, the utlity model has following advantage:
1, can effectively control the concentrated phase height and each aspect thing distribution proportion mutually of fluidisation attitude material;
2, circulation returning charge in the above suspended particulate majority of conversion zone can reach has improved reaction efficiency;
3, outer circulation returning charge amount is little, and general tower only is provided with a cyclone separator outward;
4, air-flow becomes spiral flow field by parallel flow field, can improve the mixed effect of gas one solid phase;
5, because the increasing of fluid distance, tower height can reduce, and gas speed also is improved;
6, do not need to be provided with separately heat exchange component in the tower, utilize cored screw fin flow guiding plate washer, feed refrigerant, just can effectively adjust the tower interior reaction temperature;
7, simple in structure, simplified volume is less relatively, the equipment of same ability, and its cost also can reduce.
Description of drawings:
Fig. 1 is the utility model structural representation.
Fig. 2 is Figure 1A-A cutaway view.
Fig. 3 is the helical fin structural representation.
The specific embodiment:
Referring to Fig. 1, tower body 1 is made up of cylinder, last ellipse head, lower cone three parts.The last ellipse head top of cylinder is provided with air stream outlet 13.The cylinder stage casing is provided with solid material import 2, and cylinder stage casing inwall is provided with the labyrinth helical fin flow apron of being made up of some helical fins 17 3.The cylinder hypomere is a conversion zone 7, and the cylinder hypomere is provided with material returning charge mouth 8.Be provided with reaction bed distribution grid 4, lower cone between cylinder hypomere and the lower cone and partly be provided with material outlet 5, airflow inlet 6.The air inlet of outside cyclone separator 12 is communicated with by the air stream outlet 13 of pipeline with tower body 1 top, and 12 times outlets of cyclone separator are communicated with the material returning charge mouth 8 of cylinder hypomere by pipeline.
Referring to Fig. 2, Fig. 3, helical fin 17 can also be made and bring into, export 15,16 hollow-core construction and connect with tower body 1 inwall, as the heat exchange original paper in the tower.Helical fin also can be made into solid construction.
During the utility model work, solid material enters tower body 1 from material inlet 2, and gas phase media forms parallel airflow 14 by airflow inlet 6 and after entering in the tower body 1 through reaction bed distribution grid 4.Solid matter (powder) 9 carries out the reaction of fluidisation attitude in the tower body 1 under the promotion of parallel airflow 14.The parallel airflow 14 entrained solids materials (powder) 9 that pass conversion zone 7 upwards float, under 3 effects of labyrinth helical fin flow apron, form spiral air flow 11, spiral distinguished and admirable 11 with the acting in conjunction of labyrinth sheet helical fin flow apron 3 under, its solid matter of carrying secretly (powder) 9 forms internal return reflux state 10 by labyrinth helical fin flow apron 3, make most of solid matter (powder) 9 that floats under the effect of interior cyclone centrifugal separation, conversion zone 7 backflows, a spot of subparticle 13 enters cyclone separator 12 through the gas outlet, after material returning charge mouth 8 turn back to above the conversion zone 7.Along with air velocity increases, regurgitation volume increases in the solid particle, and reaction efficiency increases, and the outer grain amount of dilute phase output tower reduces.In addition, helical fin can be made and bring into, export 15,16 hollow-core construction and connect with tower body 1 inwall, feeds refrigerant in the cavity of the labyrinth helical fin flow apron that some helical fins form, and can effectively adjust the tower interior reaction temperature.
The tower fluidized-bed reactor of interior whirlwind of the utility model band labyrinth helical fin flow apron can be widely used in the reaction of fine grained gas one solid-phase material, and the reaction of means of flue gas desulfurization of power plant.
Claims (7)
1, band labyrinth helical fin flow apron in the tower fluidized-bed reactor that backflows, the tower body (1) that comprises band reaction bed distribution grid (4), be positioned at material inlet (2), discharging opening (5), airflow inlet (6), air stream outlet (13) and material returning charge mouth (8) on the tower body, it is characterized in that being distributed with on the cylinder inboard wall labyrinth helical fin flow apron of forming by some helical fins (17) (3).
2, band as claimed in claim 1 labyrinth helical fin flow apron in the tower fluidized-bed reactor that backflows, it is characterized in that some helical fins are broken into the labyrinth and distribute.
3, band as claimed in claim 1 or 2 labyrinth helical fin flow apron in the tower fluidized-bed reactor that backflows, it is characterized in that helical fin (17) for bringing, export the hollow-core construction of (15,16) into, connects with tower body (1) inwall.
4, band as claimed in claim 1 or 2 labyrinth helical fin flow apron in the tower fluidized-bed reactor that backflows, it is characterized in that helical fin (17) is a solid construction.
5, band as claimed in claim 1 or 2 labyrinth helical fin flow apron in the tower fluidized-bed reactor that backflows, it is characterized in that labyrinth helical fin flow apron (3) is positioned on the tower body material returning charge mouth (8).
6, band as claimed in claim 1 or 2 labyrinth helical fin flow apron in the tower fluidized-bed reactor that backflows, it is characterized in that material returning charge mouth (8) is arranged on the conversion zone (7) of tower body hypomere.
7, band as claimed in claim 1 or 2 labyrinth helical fin flow apron in the tower fluidized-bed reactor that backflows, it is characterized in that air stream outlet (13) is located at the tower body top center, air stream outlet (13) is located the cyclone separator (12) that is communicated with it.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200520035081 CN2815487Y (en) | 2005-08-12 | 2005-08-12 | Internal back streaming tower fluidized_bed reactor with habyrinth helical fin diversion baffle |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200520035081 CN2815487Y (en) | 2005-08-12 | 2005-08-12 | Internal back streaming tower fluidized_bed reactor with habyrinth helical fin diversion baffle |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2815487Y true CN2815487Y (en) | 2006-09-13 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200520035081 Expired - Fee Related CN2815487Y (en) | 2005-08-12 | 2005-08-12 | Internal back streaming tower fluidized_bed reactor with habyrinth helical fin diversion baffle |
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|---|---|
| CN (1) | CN2815487Y (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101849155B (en) * | 2007-08-07 | 2013-04-10 | 伯利休斯股份有限公司 | Device and method for performing chemical and/or physical reactions between a solid material and a gas and plant for producing cement |
| CN102016474B (en) * | 2008-06-25 | 2013-09-11 | 伯利休斯股份有限公司 | Device for performing chemical and/or physical reactions between a solid material and a gas |
| CN103585934A (en) * | 2013-09-29 | 2014-02-19 | 山东百川同创能源有限公司 | Reactor suitable for cracking liquid raw materials of micro fluidized bed reaction analyzer |
| CN105087928A (en) * | 2015-10-07 | 2015-11-25 | 吉首大学 | Total-ammonia recovery type copper mine efficient chemical combination leaching device |
| CN105087922A (en) * | 2015-10-07 | 2015-11-25 | 吉首大学 | Cyclone separation ammonia total-recycle-type copper mine efficient chemical combination leaching device |
| CN105627720A (en) * | 2016-03-18 | 2016-06-01 | 李书龙 | Screw type drying tower |
| CN106185366A (en) * | 2016-08-25 | 2016-12-07 | 中国海洋石油总公司 | A kind of loading and unloading material tool assembly of tower reactor fast changeable |
| CN106636650A (en) * | 2016-12-12 | 2017-05-10 | 中南民族大学 | Three-phase reactor of rotary flow bubble tower |
| CN109999734A (en) * | 2019-04-18 | 2019-07-12 | 山东大学 | A kind of apparatus and method reverse flow heat exchange and reacted |
| CN115583688A (en) * | 2022-01-19 | 2023-01-10 | 河南理工大学 | Spiral fluidization continuous adsorption device and method based on coal gangue-based molecular sieve |
-
2005
- 2005-08-12 CN CN 200520035081 patent/CN2815487Y/en not_active Expired - Fee Related
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101849155B (en) * | 2007-08-07 | 2013-04-10 | 伯利休斯股份有限公司 | Device and method for performing chemical and/or physical reactions between a solid material and a gas and plant for producing cement |
| CN102016474B (en) * | 2008-06-25 | 2013-09-11 | 伯利休斯股份有限公司 | Device for performing chemical and/or physical reactions between a solid material and a gas |
| CN103585934A (en) * | 2013-09-29 | 2014-02-19 | 山东百川同创能源有限公司 | Reactor suitable for cracking liquid raw materials of micro fluidized bed reaction analyzer |
| CN103585934B (en) * | 2013-09-29 | 2015-09-02 | 山东百川同创能源有限公司 | Be applicable to the reactor of miniature fluidized-bed reaction analyzer liquid phase feed cracking |
| CN105087928A (en) * | 2015-10-07 | 2015-11-25 | 吉首大学 | Total-ammonia recovery type copper mine efficient chemical combination leaching device |
| CN105087922A (en) * | 2015-10-07 | 2015-11-25 | 吉首大学 | Cyclone separation ammonia total-recycle-type copper mine efficient chemical combination leaching device |
| CN105627720A (en) * | 2016-03-18 | 2016-06-01 | 李书龙 | Screw type drying tower |
| CN106185366A (en) * | 2016-08-25 | 2016-12-07 | 中国海洋石油总公司 | A kind of loading and unloading material tool assembly of tower reactor fast changeable |
| CN106636650A (en) * | 2016-12-12 | 2017-05-10 | 中南民族大学 | Three-phase reactor of rotary flow bubble tower |
| CN106636650B (en) * | 2016-12-12 | 2019-04-26 | 中南民族大学 | Eddy flow bubble tower phase reactor |
| CN109999734A (en) * | 2019-04-18 | 2019-07-12 | 山东大学 | A kind of apparatus and method reverse flow heat exchange and reacted |
| CN115583688A (en) * | 2022-01-19 | 2023-01-10 | 河南理工大学 | Spiral fluidization continuous adsorption device and method based on coal gangue-based molecular sieve |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20060913 Termination date: 20110812 |